M24 - Thermodynamic Properties

24-1

DEFINITIONS OF WORDS AND PHRASES USED IN THERMODYNAMIC

PROPERTIESAcentric factor: Afactorfrequentlyusedincorrelatingther-

modynamicpropertiesdefinedby =logPvr1.00wherePvr=reducedvaporpressureatTr=0.7.

Corresponding states:Thetheorythatproposespurecompo-nentsandmixtureshavethesamerelativethermodynamicpropertieswhenatthesamerelativethermodynamicstate.

Critical pressure:Thevaporpressureatthecriticaltempera-ture.

Critical temperature:Thetemperatureatwhichvaporandliquidpropertiesbecomeidentical.

Datum:Areferencepoint.Density:Massperunitvolumeofasubstance.Enthalpy: Heat content,H, composed of internal energy,E,

andPV.UsuallyexpressedasH=E+PV. Entropy:Athermodynamicquantity,S,definedbytheequa-

tiondS=dQ/TwhereQistheamountofheatenteringorleavingthesystemreversiblyatabsolutetemperature,T.

Ideal gas:AgaswhichfollowstheequationPV=nRTwheren=numberofmoles,andVisvolumepermole.

Irreversibility:Thedegreeofheatorworkthatislostwhenasystemistakenfromonepressureandtemperaturetoan-otherpressureand/ortemperatureandreturnedtoitsorigi-nalcondition.

Mole(s):Themassofsubstancedividedbyitsmolecularweight,expressedasmoles.

Phase envelope:Theboundariesofanareaon theP-Tdia-gramforthematerialwhichenclosestheregionwherebothvaporandliquidcoexist.

Quality: Theweight fraction of vapor in a vapor-liquidmix-ture.

Reduced pressure:Theratiooftheabsolutepressuretothecriticalpressure.

Reduced temperature:Theratiooftheabsolutetemperaturetothecriticaltemperature.

Saturated water: Water at its boiling temperature for thepressureexertedonit.

Saturated steam: Steamattheboilingtemperatureofwaterforthepressureexertedon itbutcontainingno liquidwa-ter.

Specific volume:Thevolumeofa substanceperunitmass.(Inverseofdensity.)

Thermodynamics:Thesciencewhichdealswiththeenergyofsystemsanditschangesandeffects.

H = enthalpyatdesiredconditions,kJ/kmole,orkJ/kg

H0 = idealgasstateenthalpy H00 = enthalpydatumatzeropressureandzero

temperature H0T = idealgasstateenthalpyattemperatureT HPT = enthalpyatdesiredpressureandtemperature K = Absolutetemperature,kelvin,(C+273.15) MW = molecularmass P = absolutepressure,kPa Pc = criticalorpseudocriticalpressure,kPa(abs) Pr = reducedpressure=P/Pc Pk = convergencepressureformulti-component

systems,psia T = absolutetemperature,K Tc = criticalorpseudocriticaltemperature,K Tr = reducedtemperature=T/Tc R = gasconstant,Fig.1-4 S = entropy,kJ/kmoleKorkJ/(kgK) S0 = idealgasstateentropy V = specificvolume,m3/kg

SECTION 24

Thermodynamic Properties

FIG. 24-1Nomenclature

hf = enthalpyofliquid,kJ/kg(SteamTables) hg = enthalpyofgas,kJ/kg hfg = enthalpyofvaporization(hghf)atvaporpressure sf = entropyofliquid,kJ/(kgK)(SteamTables) sg = entropyofgas,J/(kgK) sfg = entropychangeonvaporization(sgsf)atvapor

pressure vf = specificvolumeofliquid,m3/kg(SteamTables) vg = specificvolumeofgas,m3/kg vfg = specificvolumechangeonvaporization(vgvf)at

vaporpressure xi = molefractionofcomponentiinliquidphase yi = molefractionofcomponentiinvaporphaseGreek = relativedensity,dimensionless i = summationforallcomponents = acentricfactorSubscripts m = mixtureproperty i = anyonecomponentinamulticomponentmixture

This section contains thermodynamic charts, correlations,andcalculationprocedures.

Theenthalpycorrelationpresentsarigorousmethodforcal-culationofenthalpy,followedbyanexamplecalculationillus-

trating the use of the associated charts. Also included is aquicker, approximatemethod for enthalpydeterminations bytheuseoftotalenthalpycharts.Anentropycorrelationandanexamplecalculationshowingitsusearealsopresented.

24-2

ENTHALPY BEHAVIORThechangeofenthalpywithtemperatureandpressure is

complex.Predictingtheenthalpyforapurecomponentormix-ture isamulti-stepprocedure that requires information thatcanonlybeobtainedbyexperimentalmeasurement.Forpurecomponents,useofaP-HdiagramlikethoseshowninFigs.24-15to24-26isrecommended.

The enthalpy behavior ofmixes can be predicted throughthermodynamiccorrelations.Useofagoodcontemporaryequa-tionofstateisrecommendedformixtureenthalpypredictions.Fig.24-2showsgraphicallythechangeinenthalpyofthreegasstreamsandtwoliquidstreamsaspressureischangedatcon-stanttemperature.ValuesfortheplotwerecalculatedbytheSoave10versionoftheRedlich-Kwongequationofstate11.Thecurves inFig.24-2are fornophasechangeandshowtypicalbehaviorofgasphaseenthalpydecreasingandliquidphaseen-thalpyincreasingwithincreasingpressure.

Enthalpiesformixturesofrealgasesandliquidscanbepre-dictedbyhandcalculationmethods.TheonesrecommendedforusearebasedonanextensionoftheprincipleofcorrespondingstatesandareshowngraphicallyinFig.24-6and24-7.

Ideal Gas State EnthalpiesEnthalpiesforpurecomponentgasesarereadilycorrelated

asapowerseriesoftemperatureforawiderangeofcomponentsincludingallofthosethatoccurinnaturalgasstreams.TypicalvaluesfornaturalgascomponentsareplottedinFigs.24-3and24-4fortemperaturesfrom130to500C.Enthalpiesforgasmixturescanbeobtainedasthemolefractionaverageifmolarenthalpiesareused,ortheweightfractionaverageifmassen-thalpiesareused.

Many natural gas streams contain undefined, or pseudo,components. Ideal gas enthalpies for pseudo components areshowninFig.24-5.TouseFig.24-5therelativedensity,mo-lecularmassandtemperaturemustbeknown.Fig.24-5isforparaffinicmixturesandshouldnotbeusedforpseudocompo-nentsderivedfromaromaticcrudeoils.

Theenthalpydatumchoseniszeroenthalpyatzeroabso-lutepressureandzeroabsolutetemperature,thesamedatumasusedinAPIProject44.1Thechoiceofdatumisarbitraryandamatterofconvenience.Enthalpydifferences,thevaluesofin-terest,arenotaffectedbythedatumchosen.However,thesameenthalpydatumshouldbeusedforallcomponentsinanyonecalculation.

CHANGE OF ENTHALPY WITH PRESSURE

Forpurposes of correlationand calculation, the ideal andrealgasbehaviorsaretreatedseparately.Themixtureidealgasenthalpyataspecifiedtemperatureiscalculated;theenthalpychangeoftherealgasmixtureiscalculatedfromacorrelationpreparedfromexperimentalenthalpymeasurementsonavari-etyofmixtures.Thisrelationcanbeexpressedas:

HTPH00=(HT0H00)(HT0HTP) Eq 24-1where:

(HT0H00) theidealgasstateenthalpyabovethedatum,H0,atthedesiredtemperature(subscriptT),kJ/kmole

(HT0HTP) thechangeofenthalpywithpressure,given

bytheenthalphydifferencebetweentheide-algasstateenthalpyandtheenthalpyatthedesiredpressure,bothquantitiesatthespec-ifiedtemperature,kJ/kmole.

SinceH00iszeroatthechosendatum,zeroabsolutetempera-ture,Equation24-1canbewritten:

HTP=HT0(HT0HTP) Eq 24-2Whichcanbesimplifiedto:

H=H0(H0H) Eq 24-3Valuesforthechangeofenthalpywithpressureforareal

gasorliquidareobtainedfromacorrelationbasedontheprin-cipleofcorrespondingstates.2Theoriginalcorrelationwasex-tendedtolowreducedtemperatures3tocoverlowtemperaturegasprocessingapplications.ThecorrelationshowninFigs.24-6and 24-7 consists of two parts.One part gives the change ofenthalpywithpressureforasimplefluid(fluidwithzeroacen-tricfactor).Thesecondpartisacorrectionfordeviationofarealfluidfromtheidealfluidchangeofenthalpywithpressure.Thevalueof(H0H)inEq.24-3iscalculatedby:

(H0H)=RTc (H0H)(0)+ (H

0H) () Eq 24-4 RTc RTc where: [(H0H)/RTc](0) thechangeofenthalpyofasimplefluid

withpressurefromFig.24-6.[(H0H)/RTc]() deviationfromthechangeforasimple

fluidfromFig.24-7Figs.24-6and24-7canbeusedforgasandliquidmixtures.

Ifthemixtureisagas,usethelowerchartineachfigure.Forliquidsreadthevaluefromtheisothermsatthetopofthechart.Theunitsof(H0H)willdependontheunitsoftheuniversalgasconstant,R,andTc.For (H0H) inkJ/mole,R=8.3145kJ/kmoleK)andTcisinK.

ThereducedtemperatureandpressurearedefinedasTr=T/TcandPr=P/Pc,whereabsolutetemperatureandpressuremustbeused.Valuesforpurecomponentcriticaltemperature,pressureandacentricfactorareinSection23PhysicalProper-ties.Section23alsocontainsgraphsrelatingASTMdistillationtemperature,molecularweight,specificgravity(relativedensi-ty), critical temperature, and critical pressure for undefinedfractions.ThefractionacentricfactorcanbeestimatedfromEq23-17.

TouseFigs.24-6and24-7,themixturecompositionmustbeknown.Themolefractionaverage(pseudo)criticaltemperatureandpressurearecalculatedusingKaysRule4asillustratedinFig.23-7(TCm=yiTCiandPCm=yiPCi).Themolefractionav-eragemixtureenthalpyiscalculatedfrom:

Hm0=yiHi0 Eq 24-5ThevaluesofHi0areobtainedbymultiplyingtheenthalpy

valuefromFigs.24-3and24-4bythemolecularweightoftheindividualcomponent.

Themolefractionaverageacentricfactoriscalculated:m=yii Eq 24-6The information necessary to evaluate enthalpies for the

mixturefromFigs.24-3to24-7isnowknown.Useofthemeth-odwillbeclearerafterstudyofthefollowingillustrativecalcu-lation.

24-3

EXAMPLE CALCULATION USING ENTHALPY CORRELATION

AgaswiththecompositionshowninFig.24-8isat50Cand7000kPa(abs).UsingFigs.24-3and24-4calculatetheenthalpyofthegas.FollowingtheexampleinFig.23-6,themolefractionav-eragecriticaltemperatureiscalculatedas205.9K,andthepseudocriticalpressureas4613.3kPa(abs).Following thesameproce-dure,themixtureacentricfactoris0.02476andthemolaridealgasstateenthalpy11419.8kJ/kmole.Withareducedtemperatureof1.569andareducedpressureof1.517,thereadingfromFig.24-6is0.70andfromFig.24-7is0.020,whichgiveamixtureen-thalpyat50Cand7000kPa(abs)of10220.6kJ/kmole.

Ideal gas enthalpy values for each pure normal paraffincomponentwerecalculatedandusedtocalculatetheidealgasmixtureenthalpy.Theidealgasstateenthalpyequationusedformethane, ethaneandpropanewasa curve fit of thedatashowninFig.24-3.Forbutaneandheaviercomponentsafourthorder polynomial with coefficients taken from the API DataBook,TableA1.29wasused.ThefifthcoefficientreportedintheAPItablewasdroppedtoconverttothe0K,0kPaenthalpydatum.

IdealgasenthalpieswerecorrectedforpressurechangesbyinterpolatingthetabulardatausedtocompileFigs.24-6and24-7.Pressurecalculationsweremadefromreducedpressuresof0.2to13800kPa.Temperaturesrangedfrom160CtoTr=0.35minimumto320Cmaximum.

Caution:Some mixtures encountered in the calcula-tions fell inside the phase envelopes of Figs. 24-6 and 24-7. Rather than extrapolate into the phase envelopes of Figs. 24-6 and 24-7 for enthalpy pressure corrections, the total enthalpies were first generated, plotted, and then extrap-olated.

Vaporenthalpiesat1000kPawereextendedtolowertem-peraturesbyassumingtherelativeenthalpychangewithtem-peraturetobethesameasfortheidealgas.

ENTROPY CORRELATIONEntropyismostusedasaguideforinterpretingthebehav-

iorofgasesandliquidsincompressionandexpansionprocesses.TheentropyofamulticomponentmixturemaybecalculatedbycombingidealgasstateentropiesfromAPI441withtheCurlandPitzer2tablesofvaluesforthechangeofentropywithpres-sure.Entropyequationsforundefinedmixtures(pseudocompo-nents)arenotavailablebut, formostuseswhere thepseudocomponentsarepresentinsmallconcentration,theycansatis-factorilybeapproximatedbythenearestmolecularweightpar-affinhydrocarbon.

EXAMPLE CALCULATION USING ENTROPY CORRELATION

Thesamegasasintheenthalpyexample(showninFig.24-9)isat50Cand7000kPa(abs).Thepseudocriticals,acentricfactor, reduced temperature, and reduced pressure have thesamevaluesasintheenthalpyexample.Themixtureidealgasstateentropyis218.6kJ/(kmoleK).ThevaluereadfromFig.24-11is0.338andthatfromFig.24-12is0.065.Thesecombinetogive(rememberPinlnPmustbeinatmospheres)arealgasentropyof184.5kJ/(kmoleK).

ENTHALPY AND ENTROPY DATAPure CO2

ThePressure-enthalpychart forCO2inFig.24-15givesageneralpictureofenthalpyandentropychanges throughthephasesandinthecriticalregion,andallowsroughvaluestobepickedoff.

Dr. J.Ely, has publishedmany relevant papers,most re-centlyReferences12,13and14.Morerecentwork,whichalsocoversmixtureswithH2S,wassummarizedina2011paper22fromwhichthetwofollowingquotesweretaken;toseetheminfullcontext,seeSection23.

WhiletheGERG-2008equationisclearlythebestavailableEOS,itslimitationsandunreliableconvergence(within a simu-lator)makeitimpracticalforfacilitymodeling.

TheGERG-2008equationshouldthenbeusedtovalidatespecificpointstovalidatefinalequipmentdesignandven-dorofferingsdesignandperformancedata.

References15,16,17and18containmuchoftheexperimen-taldatausedbyNISTintheirEOSdevelopmentinREFPROP.Currentworkisexpectedtobepublishedlaterin2011byKunzandWagner.

Mixtures of CO2 with H2SReferences15,16,17and18(seeabove)containexperimen-

taldata.REFPROP,andtheGerg-2008equation,appeartoof-ferthebestcurrentpredictionsofmixturesdata.

Acurrent(2011)GPAResearchProject,Project042,istomea-surephysicalproperties(includingheatcapacity)inhighpres-sureacidgasstreams.H2Scontentswillrangefrom2080mol%,temperatures from 10176C, and pressures 350035 000 kPa(abs).

Oxygen, Nitrogen, and HeliumThesegasesarenowmorecommonlybeingused,orproduced,

ingasprocessingoperations.Theiruseinrocketlaunchfacilitiesled to extensivework tomeasure andmodel thermodynamic,andthedatafromthe1970sstillprovidesoneofthebestsources.References 19, 20 and 21 contain extensive tabulations (morethan100pageseach)thatincludeenthalpyandentropyvalues.

USES FOR P-H CHARTSFig. 24-13andFig. 24-14 shownear-isenthalpicpaths for

CO2blowingdownoutofapipeline,andatypicalCO2compres-sionpath.22Otherchartsandtextinthesamereferencedworkdiscuss(a)thenearer-isentropicpathforthefluidremainingina pipeline that is being blown down and (b) recycle and dis-chargecoolerfeaturesofcompressioninmoredetail.22Gener-ally,markingsuchpathsontheP-Hchartisusefulinexplain-ingandreviewingoptionsfordesignandoperations.

PhysicalpropertiesofCO2arediscussedinmoredetailinSec-tion23.NotethatthetwoexamplescopiedhereusethepreviousGPSADataBookchartversion(12thEdition).

AnothercommonuseforaP-Hchartistoplotrefrigerationcycles(using,say,thepropaneorethylenecharts).Suchillus-trationsarefrequentlyfoundinrefrigerationtextbooks.

Figures24-13and24-14 showexamplesusingaP-Hdia-gramtodisplayaprocesspath.

24-4

REFERENCES 1. APIResearchProject 44, Data onHydrocarbons andRelated

Compounds,A&MPress,CollegeStation,Texas. 2. Curl,R.F.,Jr.andPitzer,K.S.,Ind.Eng.Chem.,50,1958,p.265. 3. Chao,K.C.andGreenkorn,R.A.,GPAResearchReportRR-3,

GasProcessorsAssociation,Tulsa,Oklahoma,April1971. 4. Kay,W.B.,Ind.Eng.Chem.,28,1936,p.1014. 5. Jacoby,R.H.andYarborough,L.,TechnicalReporttoGPA,1966. 6. ASMESteamTables, 3rdEd.,Amer.Soc. ofMech.Eng.,New

York,N.Y.,1967. 7. Keenan,J.H.,Keyes,F.G.,Hill,P.G.andMoore,J.G.,Steam

Tables,JohnWiley&Sons,Inc.,NewYork,N.Y.,1969. 8. Ely,J.F.,PrivateCommunication,1985. 9. TechnicalDataBookPetroleumRefining,3rdEd.,American

PetroleumInstitute,Washington,D.C.,1977. 10. Soave,G.,EquilibriumCostantsfromaModifiedRedlich-Kwong

EquationofState,Chem.Eng.Sci.,Vol27,No.6,pp.1197-1203,1972.

11. Maddox,R.N.andMoshfeghian,M.,PrivateCommunication,1996. 12. Kiselev, S.B. and J.F. Ely, Thermodynamic Properties in the

CriticalDegion,inJSRAEThermodynamicTables.2007.p.40-44.

13. Kiselev, S.B. and J.F. Ely, HRX-SAFT Equation of State forFluidMixtures:NewAnalyticalFormulation.J.Phys.Chem.B,2007.111(43):p.15969-15975.

14. Kiselev,S.B.andJ.F.Ely,GeneralizedCrossoverDescriptionoftheThermodynamicandTransportPropertiesinPureFluidsII.Revisionandmodifications.FluidPhaseEquilib.,2007.252(1):p.57-65.

15. Kellerman, S.J., Stouffer, C.E., Gammon, B.E., Marsh, K.M.,Hall,K.R.andHolste,J.C.PVT,PhaseEquilibriaandDerivedThermodynamicPropertiesforCO2+H2SMixtures.

16. Bailey,D.M.,Liu,C.-H.,Holste,P.T.andEubank,P.T.EnergyFunctions forH2S,Part3:Near-equimolarMixturewithCO2,Hydro. Process. Pet. Ref., Volume 67, Number 1, pp. 73-74,1987.

17. Liu,C.H.ExperimentalDensities,EntropiesandEnergies forPureH2SandEquimolarMixturesofH2S/CH4andH2S/CO2Be-tween300and500K,BMasterofScience,GraduateCollegeofTexasA&MUniversity,1985.

18. Bailey,D.M.,Liu,C.-H.,Holste,J.C.,Hall,K.R.,Eubank,P.T.,Marsh,K.M.,ThermodynamicPropertiesofPureHydrogenSul-fideandMixturesContainingHydrogenSulfidewithMethane,Carbon Dioxide, Methylcyclohexane and Toluene, GPA Re-searchReportNo.107,1987.

19. McCartney,R.D.andWeber,L.A.,ThermophysicalPropertiesofOxygenFromtheFreezingLiquidLineto600RforPressuresto5000psia.NBSTechnicalNote384,1971

20. McCartney,R.D.,ThermophysicalPropertiesofHelium-4from2to1500KwithPressuresto1000AtmospheresNBSTechnicalNote631,1973.

21. Jacobsen,R.T.,Stewart,R.B.,McCarty,R.D.,andHanley,H.J.M., Thermophysical Properties of Nitrogen from the FusionLineto3500R(1944K)forPressuresto150,000psia(10342x105N/m2).NBSTechnicalNote648,1973.

22. Cunningham,C.R.,Miller,T,andFriedman,B.,CO2Compres-sionFacilityandPipelineDesign91stAnnualGPAConvention2011.

BIBLIOGRAPHYCanjar,L.N.andManning,F.S.,ThermodynamicPropertiesandRe-duced Correlations of Gases, Gulf Publishing Co., Houston, Texas,1967.Kesler,M.G.andLee,B.I.,ImprovePredictionofEnthalpyofFrac-tions,HydrocarbonProcessing,55,1976,pp.153-158.Lee,M.C.,Ratcliffe,A.E.,Maddox,R.D.,Parham,W.F.andMaddox,R.N.,HeatCapacityDeterminedforCrudeFractions,HydrocarbonProcessing,June1978,pp.187-189.Maddox,R.N.andL.Lilly,GasConditioningandProcessing,Vol.3,CampbellPetroleumSeriesInc.,Norman,Oklahoma,1990.PropertiesforLightPetroleumSystems,GulfPublishingCo.,Hous-ton,Texas,1973.TechnicalDataBookPetroleumRefining,3rdEd.,AmericanPetro-leumInstitute,Washington,D.C.,1977.Reid,R.D.,Prausnitz,J.M.andSherwood,T.K.,ThePropertiesofGasesandLiquids,3rdEd.,McGraw-HillBookCo.,NewYork,N.Y.,1977.Starling,K.E.,FluidThermodynamicPropertiesforLightPetroleumSystems,GulfPublishingCo.,Houston,Texas1973.VanNess,H.C.andAbbott,M.M.,ClassicalThermodynamicsofNon-ElectrolyteSolutions,McGraw-Hill,N.Y.,1982.Weber,J.H.,PredictLatentHeatsofVaporization,ChemicalEngi-neering,Jan.14,1980.Wormald,C.J.,ThermoDataforSteam/Hydrocarbons,HydrocarbonProcessing,May1982,pp.137-141.Yu,W.C.,Lee,H.M.andLigon,R.M.,PredictedHighPressureProp-erties,HydrocarbonProcessing,Jan.1982,pp.171-178.

24-5

FIG. 24-2Influence of Pressure on Enthalpy for Typical Natural Gas Streams

24-6

FIG. 24-3Ideal-Gas-State Enthalpy of Pure Components

24-7

FIG. 24-4Ideal-Gas-State Enthalpy of Pure Components

24-8

FIG. 24-5Ideal-Gas-State Enthalpy of Petroleum Fractions

24-9

FIG. 24-6Effect of Pressure on Enthalpy (Simple Fluid)

24-10

FIG. 24-7Effect of Pressure on Enthalpy (Correction for Real Fluids)

24-11

Component Mole Fraction Molecular MassCritical Temp. K

Critical Pressure kPa Acentric Factor

Ideal Gas Enthalpy kJ/kg

Methane 0.9010 16.04 190.6 4599.0 0.0108 682CarbonDioxide 0.0106 44.01 304.1 7374.0 0.2667 234Ethane 0.0499 30.07 305.4 4880.0 0.0972 442Propane 0.0187 44.10 369.8 4240.0 0.1515 381i-Butane 0.0065 58.12 407.8 3640.0 0.1852 357n-Butane 0.0045 58.12 425.1 3784.0 0.1981 381i-Pentane 0.0017 72.15 460.4 3381.0 0.2286 357n-Pentane 0.0019 72.15 469.7 3365.0 0.2510 370Hexane 0.0052 86.18 506.4 3030.0 0.2990 326

IDEALGASSTATEENTHALPYkJ/kmole 11419.8PSEUDOCRITICALTEMPERATUREK 205.9REDUCEDTEMPERATURE 1.569PSEUDOCRITICALPRESSUREkPa(abs) 4613.3REDUCEDPRESSURE 1.517MOLEFRACTIONAVERAGEACENTRICFACTOR 0.02476

[(H0H)/RTC](0)fromFig.24-6 0.70

[(H0H)/RTC]()fromFig.24-7 0.02

[(H0H)m/RTC]=[(H0H)/RTC](0)+[wm[(H0H)/RTC]() 0.7005

(H0H)m,kJ/kmole 1199.2

H,kJ/kmole 10220.6

NOTE: IdealGasEnthalpyforHexanefromthe12thEditionoftheDataBook(Fig.24-9). WichertandAzizcorrectionnotappliedtocriticalproperties.

FIG. 24-8Example Enthalpy Calculation

24-12

Component Mole Fraction Molecular WeightCritical Temp. K

Critical Pressure kPa Acentric Factor

Ideal Gas Entropy kJ/(kg K)

Methane 0.9010 16.04 190.6 4599.0 0.0108 13.19CarbonDioxide 0.0106 44.01 304.1 7374.0 0.2667 4.90Ethane 0.0499 30.07 305.4 4880.0 0.0972 8.50Propane 0.0187 44.10 369.8 4240.0 0.1515 6.80i-Butane 0.0065 58.12 407.8 3640.0 0.1852 5.83n-Butane 0.0045 58.12 425.1 3784.0 0.1981 5.58i-Pentane 0.0017 72.15 460.4 3381.0 0.2286 5.29n-Pentane 0.0019 72.15 469.7 3365.0 0.2510 5.20Hexane 0.0052 86.18 506.4 3030.0 0.2990 5.02

IDEALGASSTATEENTROPYkJ/(kmoleK) 218.6PSEUDOCRITICALTEMPERATUREK 205.9REDUCEDTEMPERATURE 1.569PSEUDOCRITICALPRESSUREkPa(abs 4613.3REDUCEDPRESSURE 1.517MOLEFRACTIONAVERAGEACENTRICFACTOR 0.02476

[(S0S)/R](0)fromFig.24-11 0.338

[(S0S)/R]()fromFig.24-12 0.065

lnP(Pinatmospheres) 4.2353

(S0S)=R (S0S) (0) +w

(S0S) () +lnP 38.025 R R

R yiln(yi) 3.935

Smo=( yiSioR yilnyi) 222.5

Sm=[Smo(SmoSm)] 184.5NOTE: EntropyforHexanewasestimated. WichertandAzizcorrectionnotappliedtocriticalproperties.

FIG. 24-9Example Entropy Calculation

24-13

FIG. 24-10Ideal-gas-state Entropy of Pure Components

24-14

FIG. 24-11Effect of Pressure on Entropy (Simple Fluid)

24-15

FIG. 24-12Effect of Pressure on Entropy (Correction for Real Fluids)

24-16

Notethatblowd

ownfro

mhighertemperatures,representedbyth

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htha

ndpath,rem

ainswith

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hileblowd

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gion).

FIG. 24-13Sample Isenthalpic Blowdown Paths

Span

,R.a

ndW

agner,W.,ANew

Equ

ationofStateforC

arbon

DioxideCoveringtheFluidRe

gionfrom

theTriple-PointTem

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ressuresupto800M

Pa,J.Phy

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ata,

25(6):1

509-1596,1

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CARB

ON

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IDE

24-17

FIG. 24-14Sample Multi-Stage Compression Path with Interstage Cooling and Recycle

Last s

tage

rec

ycle

will

form

liqui

d in

inte

rsta

ges

cru

bber

Span

,R.a

ndW

agner,W.,ANew

Equ

ationofStateforC

arbon

DioxideCoveringtheFluidRe

gionfrom

theTriple-PointTem

perature

to1100KatP

ressuresupto800M

Pa,J.Phy

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ata,

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CARB

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IDE

24-19

FIG. 24-15 Carbon Dioxide P-H Diagram

FIG. 24-16 Nitrogen P-H Diagram

Span, R., Lemmon, E.W., Jacobsen, R.T, Wagner, W., and Yokozeki, A. A Reference Quality Thermodynamic Property Formulation for Nitrogen, J. Phys. Chem. Ref. Data, 29(6):1361-1433, 2000.

24-20 NITROGEN

Setzmann, U. and Wagner, W., A New Equation of State and Tables of Thermodynamic Properties for Methane Covering the Range from the Melting Line to 625 K at Pressures up to 1000 MPa, J. Phys. Chem. Ref. Data, 20(6):1061-1151, 1991.

24-21

FIG. 24-17 Methane P-H Diagram

METHANE

Friend, D.G., Ingham, H., and Ely, J.F., Thermophysical Properties of Ethane, J. Phys. Chem. Ref. Data, 20(2):275-347, 1991.

24-22

FIG. 24-18 Ethane P-H Diagram

ETHANE

Smukala, J., Span, R. and Wagner, W. A New Equation of State for Ethylene Covering the Fluid Region for Temperatures from the Melting Line to 450 K at Pressures up to 300 MPa, J. Phys. Chem. Ref. Data, 29(5):1053-1122, 2000.

24-23

FIG. 24-19 Ethylene P-H Diagram

ETHYLENE

Miyamoto, H., and Watanabe, K., A Thermodynamic Property Model for Fluid-phase Propane, Int. J. Thermophys., 21(5):1045-1072, 2000.

24-24

FIG. 24-20 Propane P-H Diagram

PROPANE

Angus, S., Armstrong, B., and de Reuck, K.M., International Thermodynamic Tables of the Fluid State-7 Propylene, International Union of Pure and Applied Chemistry, Pergamon Press, Oxford, 1980..

24-25

FIG. 24-21 Propylene P-H Diagram

PROPYLENE

Miyamoto, H. and Watanabe, K. A Thermodynamic Property Model for Fluid-Phase Isobutane, Int. J. Thermophys., 23(2):477-499, 2002.

24-26

FIG. 24-22 i-Butane P-H Diagram

I-BUTANE

Miyamoto, H. and Watanabe, K. A Thermodynamic Property Model for Fluid-Phase n-Butane, Int. J. Thermophys., 22(2):459-475, 2001.

24-27

FIG. 24-23 n-Butane P-H Diagram

N-BUTANE

Lemmon, E.W. and Span, R., preliminary equation, 2003.

24-28

FIG. 24-24 i-Pentane P-H Diagram

I-PENTANE

Span, R., Multiparameter Equations of State An Accurate Source of Thermodynamic Property Data, Springer, Berlin, Heidelberg, New York, 2000.

24-29

FIG. 24-25 n-Pentane P-H Diagram

N-PENTANE

Schmidt, R. and Wagner, W.,A New Form of the Equation of State for Pure Substances and its Application to Oxygen, Fluid Phase Equilibria, 19:175-200, 1985.

24-30

FIG. 24-26 Oxygen P-H Diagram

OXYGEN

24-31

Subs

tanc

e TP

T N

BP

TC

P

C

RH

OC

A

CE

N

TMIN

TM

AX

PM

AX

RH

OM

AX

K

K

K

kP

a M

ol/L

K

K

kPa

Mol

/L

Metha

ne

90.6941

111.667

190.564

4599.2

10.139

.01142

90.6941

625

1000000

40.072

Etha

ne

90.352

184.552

305.33

4871.8

6.87

.0993

90.352

625

70000

22.419

Propan

e85.48

231.06

369.825

4247.09

4.95514

.1524

85.48

623

103000

17.41

Isobutan

e113.56

261.48

407.817

3640.0

3.860

.185

113.56

573

35000

12.90

n-Bu

tane

134.87

272.6

425.125

3796.0

3.920

.2

134.87

589

69000

13.15

Isopentane

112.65

300.97

460.35

3396.0

3.271

.2296

112.65

600

1000000

10.93

n-Pe

ntan

e143.47

309.21

469.7

3370.0

3.2156

.251

143.47

600

100000

10.57

Ethy

lene

103.986

169.379

282.35

5041.8

7.637

.0866

103.986

450

260000

26.67

Propylene

87.95

225.46

365.57

4664.6

5.3086

.1408

100.0

600

200000

17.95

Nitr

ogen

63.151

77.355

126.192

3395.8

11.1839

.0372

63.151

2000

2200000

53.15

Oxygen

54.361

90.1878

154.581

5043.0

13.63

.0222

54.361

1000

82000

43.348

CarbonDioxide

216.592

194.75

304.1282

7377.3

10.6249

.22394

216.592

1100

800000

37.24

Virtua

lMaterialsGroup

gratefully

acknowledgesth

eassistan

ceprovidedbyDr.Er

icLem

monand

Dr.Micha

elFrenk

elfrom

theNationa

lInstitute

ofStand

ardsand

Techn

ology(N

IST)fortheirassistanceinth

epreparationofth

eP-HDiagram

spresentedinFig.24-15th

roug

hFig.24-26and

asthe

basisforFigs.24-13an

d24-14.

Ack

now

ledg

men

ts

TPT

Triplepointte

mperature

NBP

NormalBoilin

gPo

int

TC

CriticalT

emperature

PC

CriticalP

ressure

RHOC

CriticalD

ensity

ACEN

Ac

entricFactor

TMIN

Minim

umRecom

mendedTe

mperature

TMAX

Maxim

umRecom

mendedTe

mperature

PMAX

Maxim

umRecom

mended

Pressure

RHOMAX

Maxim

umRecom

mendedDensity

R

efer

ence

Tem

pera

ture

R

efer

ence

Pre

ssur

e

Val

ue (C

) D

atab

ase

Val

ue (k

Pa)

D

atab

ase

Etha

ne

182.80

NIST

1.131E

03

TRC

Metha

ne

182.46

NIST

1.170E

+01

TRC

N2

210.00

NIST

1.252E

+01

TRC

CO2

56.56

NIST

5.187E

+02

TRC

Ethy

lene

169.16

NIST

1.260E

01

TRC

Propan

e187.67

NIST

1.685E

07

TRC

Propylene

173.15

NIST

9.332E

07

TRC

I-Butan

e159.59

NIST

1.206E

05

TRC

n-Bu

tane

138.28

NIST

6.736E

04

TRC

I-Pentane

159.90

TRC

1.214E

07

TRC

n-Pe

ntan

e129.68

NIST

7.632E

05

TRC

Oxygen

218.79

NIST

1.500E

01

TRC

24-32

FIG. 24-27Thermodynamic Properties of Water

24-33

FIG. 24-28Thermodynamic Properties of Water

24-34

Temp. C T

Press. kPa

P

Specific Volume Internal Energy Enthalpy EntropySat.

Liquid vf

Sat. Vapor

vg

Sat. Liquid

uf

Evap.

ufg

Sat. Vapor

ug

Sat. Liquid

hf

Evap.

hfg

Sat. Vapor

hg

Sat. Liquid

sf

Evap.

sfg

Sat. Vapor

sg

0.01 0.6113 0.001000 206.14 .00 2375.3 2375.3 .01 2501.3 2501.4 .0000 9.1562 9.1562 5 0.8721 0.001000 147.12 20.97 2361.3 2382.3 20.98 2489.6 2510.6 .0761 8.9496 9.0257 10 1.2276 0.001000 106.38 42.00 2347.2 2389.2 42.01 2477.7 2519.8 .1510 8.7498 8.9008 15 1.7051 0.001001 77.93 62.99 2333.1 2396.1 62.99 2465.9 2528.9 .2245 8.5569 8.7814 20 2.339 0.001002 57.79 83.95 2319.0 2402.9 83.96 2454.1 2538.1 .2966 8.3706 8.6672 25 3.169 0.001003 43.36 104.88 2304.9 2409.8 104.89 2442.3 2547.2 .3674 8.1905 8.5580 30 4.246 0.001004 32.89 125.78 2290.8 2416.6 125.79 2430.5 2556.3 .4369 8.0164 8.4533 35 5.628 0.001006 25.22 146.67 2276.7 2423.4 146.68 2418.6 2565.3 .5053 7.8478 8.3531 40 7.384 0.001008 19.52 167.36 2262.6 2430.1 167.37 2406.7 2574.3 .5725 7.6845 8.2570 45 9.593 0.001010 15.26 188.44 2248.4 2436.8 188.45 2394.8 2583.2 .6387 7.5261 8.1648 50 12.349 0.001012 12.03 209.32 2234.2 2443.5 209.33 2382.7 2592.1 .7038 7.3725 8.0763 55 15.758 0.001015 9.568 230.21 2219.9 2450.1 230.23 2370.7 2600.9 .7679 7.2234 7.9913 60 19.940 0.001017 7.671 251.11 2205.5 2456.6 251.13 2358.5 2609.6 .8312 7.0784 7.9096 65 25.03 0.001020 6.197 272.02 2191.1 2463.1 272.06 2346.2 2618.3 .8935 6.9375 7.8310 70 31.19 0.001023 5.042 292.95 2176.6 2469.6 292.98 2333.8 2626.8 .9549 6.8004 7.7553 75 38.58 0.001026 4.131 313.90 2162.0 2475.9 313.93 2321.4 2635.3 1.0155 6.6669 7.6824 80 47.39 0.001029 3.407 334.86 2147.4 2482.2 334.91 2308.8 2643.7 1.0753 6.5369 7.6122 85 57.83 0.001033 2.828 355.84 2132.6 2488.4 355.90 2296.0 2651.9 1.1343 6.4102 7.5445 90 70.14 0.001036 2.361 376.85 2117.7 2494.5 376.92 2283.2 2660.1 1.1925 6.2866 7.4791 95 84.55 0.001040 1.982 397.88 2102.7 2500.6 397.96 2270.2 2668.1 1.2500 6.1659 7.4159100 101.35 0.001044 1.6729 418.94 2087.6 2506.5 419.04 2257.0 2676.1 1.3069 6.0480 7.3549105 120.82 0.001048 1.4194 440.02 2072.3 2512.4 440.15 2243.7 2683.8 1.3630 5.9328 7.2958110 143.27 0.001052 1.2102 461.14 2057.0 2518.1 461.30 2230.2 2691.5 1.4185 5.8202 7.2387115 169.06 0.001056 1.0366 482.30 2041.4 2523.7 482.48 2216.5 2699.0 1.4734 5.7100 7.1833120 198.53 0.001060 0.8919 503.50 2025.8 2529.3 503.71 2202.6 2706.3 1.5276 5.6020 7.1296125 232.1 0.001065 0.7706 524.74 2009.9 2534.6 524.99 2188.5 2713.5 1.5813 5.4962 7.0775130 270.1 0.001070 0.6685 546.02 1993.9 2539.9 546.31 2174.2 2720.5 1.6344 5.3925 7.0269135 313.0 0.001075 0.5822 567.35 1977.7 2545.0 567.69 2159.6 2727.3 1.6870 5.2907 6.9777140 361.3 0.001080 0.5089 588.74 1961.3 2550.0 589.13 2144.7 2733.9 1.7391 5.1908 6.9299145 415.4 0.001085 0.4463 610.18 1944.7 2554.9 610.63 2129.6 2740.3 1.7907 5.0926 6.8833150 475.8 0.001091 0.3928 631.68 1927.9 2559.5 632.20 2114.3 2746.5 1.8418 4.9960 6.8379155 543.1 0.001096 0.3468 653.24 1910.8 2564.1 653.84 2098.6 2752.4 1.8925 4.9010 6.7935160 617.8 0.001102 0.3071 674.87 1893.5 2568.4 675.55 2082.6 2758.1 1.9427 4.8075 6.7502165 700.5 0.001108 0.2727 696.56 1876.0 2572.5 697.34 2066.2 2763.5 1.9925 4.7153 6.7078170 791.7 0.001114 0.2428 718.33 1858.1 2576.5 719.21 2049.5 2768.7 2.0419 4.6244 6.6663175 892.0 0.001121 0.2168 740.17 1840.0 2580.2 741.17 2032.4 2773.6 2.0909 4.5347 6.6256180 1002.1 0.001127 0.19405 762.09 1821.6 2583.7 763.22 2015.0 2778.2 2.1396 4.4461 6.5857185 1122.7 0.001134 0.17409 784.10 1802.9 2587.0 785.37 1997.1 2782.4 2.1879 4.3586 6.5465190 1254.4 0.001141 0.15654 806.19 1783.8 2590.0 807.62 1978.8 2786.4 2.2359 4.2720 6.5079195 1397.8 0.001149 0.14105 828.37 1764.4 2592.8 829.98 1960.0 2790.0 2.2835 4.1863 6.4698200 1553.8 0.001157 0.12736 850.65 1744.7 2595.3 852.45 1940.7 2793.2 2.3309 4.1014 6.4323205 1723.0 0.001164 0.11521 873.04 1724.5 2597.5 875.04 1921.0 2796.0 2.3780 4.0172 6.3952210 1906.2 0.001173 0.10441 895.53 1703.9 2599.5 897.76 1900.7 2798.5 2.4248 3.9337 6.3585215 2104. 0.001181 0.09479 918.14 1682.9 2601.1 920.62 1879.9 2800.5 2.4714 3.8507 6.3221220 2318. 0.001190 0.08619 940.87 1661.5 2602.4 943.62 1858.5 2802.1 2.5178 3.7683 6.2861225 2518. 0.001199 0.07849 963.73 1639.6 2603.3 966.78 1836.5 2803.3 2.5639 3.6863 6.2503230 2795. 0.001209 0.07158 986.74 1617.2 2603.9 990.12 1813.8 2804.0 2.6099 3.6047 6.2146235 3060. 0.001219 0.06537 1009.89 1594.2 2604.1 1013.62 1790.5 2804.2 2.6558 3.5233 6.1791240 3344. 0.001229 0.05976 1033.21 1570.8 2604.0 1037.32 1766.5 2803.8 2.7015 3.4422 6.1437245 3618. 0.001240 0.05471 1056.71 1546.7 2603.4 1061.23 1741.7 2803.0 2.7472 3.3612 6.1083250 3973. 0.001251 0.050.13 1080.39 1522.0 2602.4 1085.36 1716.2 2801.5 2.7927 3.2802 6.0730255 4319. 0.001263 0.04598 1104.28 1496.7 2600.9 1109.73 1689.8 2799.5 2.8383 3.1992 6.0375260 4688. 0.001276 0.04221 1128.39 1470.6 2599.0 1134.37 1662.5 2796.9 2.8838 3.1181 6.0019265 5081. 0.001289 0.03877 1152.74 1443.9 2596.6 1159.28 1634.4 2793.6 2.9294 3.0368 5.9662270 5499. 0.001302 0.03564 1177.36 1416.3 2593.7 1184.51 1605.2 2789.7 2.9751 2.9551 5.9301275 5942. 0.001317 0.03279 1202.25 1387.9 2590.2 1210.07 1574.9 2785.0 3.0208 2.8730 5.8938280 6412. 0.001332 0.03017 1227.46 1358.7 2586.1 1235.99 1543.6 2779.6 3.0668 2.7903 5.8571285 6909. 0.001348 0.02777 1253.00 1328.4 2581.4 1262.31 1511.0 2773.3 3.1130 2.7070 5.8199290 7436. 0.001366 0.02557 1278.92 1297.1 2576.0 1289.07 1477.1 2766.2 3.1594 2.6227 5.7821295 7993. 0.001384 0.02354 1305.2 1264.7 2569.9 1316.3 1441.8 2758.1 3.2062 2.5375 5.7437300 8581. 0.001404 0.02167 1332.0 1231.0 2563.0 1344.0 1404.9 2749.0 3.2534 2.4511 5.7045305 9202. 0.001425 0.019948 1359.3 1195.9 2555.2 1372.4 1366.4 2738.7 3.3010 2.3633 5.6643310 9856. 0.001447 0.018350 1387.1 1159.4 2546.4 1401.3 1326.0 2727.3 3.3493 2.2737 5.6230315 10547. 0.001472 0.016867 1415.5 1121.1 2536.6 1431.0 1283.5 2714.5 3.3982 2.1821 5.5804320 11274. 0.001499 0.015488 1444.6 1080.9 2525.5 1461.5 1238.6 2700.1 3.4480 2.0882 5.5362330 12845. 0.001561 0.012996 1505.3 993.7 2498.9 1525.3 1140.6 2665.9 3.5507 1.8909 5.4417340 14586. 0.001638 0.010797 1570.3 894.3 2464.6 1594.2 1027.9 2622.0 3.6594 1.6763 5.3357350 16513. 0.001740 0.008813 1641.9 776.6 2418.4 1670.6 893.4 2563.9 3.7777 1.4335 5.2112360 18651. 0.001893 0.006945 1725.2 626.3 2351.5 1760.5 720.5 2481.0 3.9147 1.1379 5.0526370 21030. 0.002213 0.004925 1844.0 384.5 2228.5 1890.5 441.6 2332.1 4.1106 .6865 4.7971374.14 22090. 0.003155 0.003155 2029.6 0 2029.6 2099.3 0 2099.3 4.4298 0 4.4298

FIG. 24-29Saturated Steam: Temperature Table

24-35

SymbolsUsedinSteamTables:Ppressure,kPa(abs);Tthermodynamictemperature,C;vspecificvolume,m3/kg;uspecificinternalenergy,kJ/kg;hspecificenthalpy,kJ/kg sspecificentropy,kJ/(kgK) AdaptedfromJosephH.Keenan,FrederickG.Keyes,PhilipG.Hill,andJoanG.Moore,SteamTables,(NewYork:JohnWiley&Sons,Inc.,1969).

Press. KPa

P

Temp. C T

Specific Volume Internal Energy Enthalpy Entropy

Sat. Liquid

vf

Sat. Vapor

vg

Sat. Liquid

uf

Evap.

ufg

Sat. Vapor

ufg

Sat. Liquid

hfg

Evap.

hfg

Sat. Vapor

hg

Sat. Liquid

sf

Evap.

sfg

Sat. Vapor

sg 0.6113 0.01 0.001000 206.14 00 2375.3 2375.3 01. 2501.3 2501.4 .0000 9.1562 9.1562 1.0 6.98 0.001000 129.21 29.30 2355.7 2385.0 29.30 2484.9 2514.2 .1059 8.8697 8.9756 1.5 13.03 0.001001 87.98 54.71 2338.6 2393.3 54.71 2470.6 2525.3 .1957 8.6322 8.8279 2.0 17.50 0.001001 67.00 73.48 2326.0 2399.5 73.48 2460.0 2533.5 .2607 8.4629 8.7237 2.5 21.08 0.001002 54.25 88.48 2315.9 2404.4 88.49 2451.6 2540.0 .3120 8.3311 8.6432 3.0 24.08 0.001003 45.67 101.04 2307.5 2408.5 101.05 2444.5 2545.5 .3545 8.2231 8.5776 4.0 28.96 0.001004 34.80 121.45 2293.7 2415.2 121.46 2432.9 2554.4 .4226 8.0520 8.4746 5.0 32.88 0.001005 28.19 137.81 2282.7 2420.5 137.82 2423.7 2561.5 .4764 7.9187 8.3951 7.5 40.29 0.001008 19.24 168.78 2261.7 2430.5 168.79 2406.0 2574.8 .5764 7.6750 8.2515 10 45.81 0.001010 14.67 191.82 2246.1 2437.9 191.83 2392.8 2584.7 .6493 7.5009 8.1502 15 53.97 0.001014 10.02 225.92 2222.8 2448.7 225.94 2373.1 2599.1 .7549 7.2536 8.0085 20 60.05 0.001017 7.649 251.38 2205.4 2456.7 251.40 2358.3 2609.7 .8320 7.0766 7.9085 25 64.97 0.001020 6.204 271.90 2191.2 2463.1 271.93 2346.3 2618.2 .8931 6.9383 7.8314 30 69.10 0.001022 5.229 289.20 2179.2 2468.4 289.23 2336.1 2625.3 .9439 6.8247 7.7686 40 75.87 0.001027 3.993 317.53 2159.5 2477.0 317.58 2319.2 2636.8 1.0259 6.6441 7.6700 50 81.33 0.001030 3.240 340.44 2143.4 2483.9 340.49 2305.4 2645.9 1.0910 6.5029 7.5939 75 91.78 0.001037 2.217 384.31 2112.4 2496.7 384.39 2278.6 2663.0 1.2130 6.2434 7.4564 100 99.63 0.001043 1.6940 417.36 2088.7 2506.1 417.46 2258.0 2675.5 1.3026 6.0368 7.3594 125 105.99 0.001048 1.3749 444.19 2069.3 2513.5 444.32 2241.0 2685.4 1.3740 5.9104 7.2844 150 111.37 0.001053 1.1593 466.94 2052.7 2519.7 467.11 2226.5 2693.6 1.4336 5.7897 7.2233 175 116.06 0.001057 1.0036 486.80 2038.1 2524.9 486.99 2213.6 2700.6 1.4849 5.6868 7.1717 200 120.23 0.001061 0.8857 504.49 2025.0 2529.5 504.70 2201.9 2706.7 1.5301 5.5970 7.1271 225 124.00 0.001064 0.7933 520.47 2013.1 2533.6 520.72 2191.3 2712.1 1.5706 5.5173 7.0878 250 127.44 0.001067 0.7187 535.10 2002.1 2537.2 535.37 2181.5 2716.9 1.6072 5.4455 7.0527 275 130.60 0.001070 0.6573 548.59 1991.9 2540.5 548.89 2172.4 2721.3 1.6408 5.3801 7.0209 300 133.55 0.001073 0.6058 561.15 1982.4 2543.6 561.47 2163.8 2725.3 1.6718 5.3201 6.9919 325 136.30 0.001076 0.5620 572.90 1973.5 2546.4 573.25 2155.8 2729.0 1.7006 5.2646 6.9652 350 138.88 0.001079 0.5243 583.95 1965.0 2548.9 584.33 2148.1 2732.4 1.7275 5.2130 6.9405 375 141.32 0.001081 0.4914 594.40 1956.9 2551.3 594.81 2140.8 2735.6 1.7528 5.1647 6.9175 400 143.63 0.001084 0.4625 604.31 1949.3 2553.6 604.74 2133.8 2738.6 1.7766 5.1193 6.8959 450 147.93 0.001088 0.4140 622.77 1934.9 2557.6 623.25 2120.7 2743.9 1.8207 5.0359 6.8565 500 151.86 0.001093 0.3749 639.68 1921.6 2561.2 640.23 2108.5 2748.7 1.8607 4.9606 6.8213 550 155.48 0.001097 0.3427 655.32 1909.2 2564.5 655.93 2097.0 2753.0 1.8973 4.8920 6.7893 600 158.85 0.001101 0.3157 669.90 1897.5 2567.4 670.56 2086.3 2756.8 1.9312 4.8288 6.7600 650 162.01 0.001104 0.2927 683.56 1886.5 2570.1 684.28 2076.0 2760.3 1.9627 4.7703 6.7331 700 164.97 0.001108 0.2729 696.44 1876.1 2572.5 697.22 2066.3 2763.5 1.9922 4.7158 6.7080 750 167.78 0.001112 0.2556 708.64 1866.1 2574.7 709.47 2057.0 2766.4 2.0200 4.6647 6.6847 800 170.43 0.001115 0.2404 720.22 1856.6 2576.8 721.11 2048.0 2769.1 2.0462 4.6166 6.6628 850 172.96 0.001118 0.2270 731.27 1847.4 2578.7 732.22 2039.4 2771.6 2.0710 4.5711 6.6421 900 175.38 0.001121 0.2150 741.83 1838.6 2580.5 742.83 2031.1 2773.9 2.0946 4.5280 6.6226 950 177.69 0.001124 0.2042 751.95 1830.2 2582.1 753.02 2023.1 2776.1 2.1172 4.4869 6.6041 1000 179.91 0.001127 0.19444 761.68 1822.0 2583.6 762.81 2015.3 2778.1 2.1387 4.4478 6.5865 1100 184.09 0.001133 0.17753 780.09 1806.3 2586.4 781.34 2000.4 2781.7 2.1792 4.3744 6.5536 1200 187.99 0.001139 0.16333 797.29 1791.5 2588.8 798.65 1986.2 2784.8 2.2166 4.3067 6.5233 1300 191.64 0.001144 0.15125 813.44 1777.5 2591.0 814.93 1972.7 2787.6 2.2515 4.2438 6.4953 1400 195.07 0.001149 0.14084 828.70 1764.1 2592.8 830.30 1959.7 2790.0 2.2842 4.1850 6.4693 1500 198.32 0.001154 0.13177 843.16 1751.3 2594.5 844.89 1947.3 2792.2 2.3150 4.1298 6.4448 1750 205.76 0.001166 0.11349 876.46 1721.4 2597.8 878.50 1917.9 2796.4 2.3851 4.0044 6.3896 2000 212.42 0.001177 0.09963 906.44 1693.8 2600.3 908.79 1890.7 2799.5 2.4474 3.8935 6.3409 2250 218.45 0.001187 0.08875 933.83 1668.2 2602.0 936.49 1865.2 2801.7 2.5035 3.7937 6.2972 2500 223.99 0.001197 0.07998 959.11 1644.0 2603.1 962.11 1841.0 2803.1 2.5547 3.7028 6.2575 3000 233.90 0.001217 0.06668 1004.78 1599.3 2604.1 1008.42 1795.7 2804.2 2.6457 3.5412 6.1869 3500 242.60 0.001235 0.05707 1045.43 1558.3 2603.7 1049.75 1753.7 2804.2 2.7253 3.4000 6.1253 4000 250.40 0.001252 0.04978 1082.31 1520.0 2602.3 1087.31 1714.1 2801.4 2.7964 3.2737 6.0701 5000 263.99 0.001286 0.03944 1147.81 1449.3 2597.1 1154.23 1640.1 2794.3 3.9202 3.0532 5.9734 6000 275.64 0.001319 0.03244 1205.44 1384.3 2589.7 1213.35 1571.0 2784.3 3.0267 2.8625 5.8892 7000 285.88 0.001351 0.02737 1257.55 1323.0 2580.5 1267.00 1505.1 2772.1 3.1211 2.6922 5.8133 8000 295.06 0.001384 0.02352 1305.57 1264.2 2569.8 1316.64 1441.3 2758.0 3.2068 2.5364 5.7432 9000 303.40 0.001418 0.02048 1350.51 1207.3 2557.8 1363.26 1378.9 2742.1 3.2858 2.3915 5.677210000 311.06 0.001452 0.018026 1393.04 1151.4 2544.4 1407.56 1317.1 2724.7 3.3596 2.2544 5.614111000 318.15 0.001489 0.015987 1433.7 1096.0 2529.8 1450.1 1255.5 2705.6 3.4295 2.1233 5.552712000 324.75 0.001527 0.014263 1473.0 1040.7 2513.7 1491.3 1193.6 2684.9 3.4962 1.9962 5.492413000 330.93 0.001567 0.012780 1511.1 985.0 2496.1 1531.5 1130.7 2662.2 3.5606 1.8718 5.432314000 336.75 0.001611 0.011485 1548.6 928.2 2476.8 1571.1 1066.5 2637.6 3.6232 1.7485 5.371715000 342.24 0.001658 0.010337 1585.0 869.8 2455.5 1610.5 1000.0 2610.5 3.6848 1.6249 5.309816000 347.44 0.001711 0.009306 1622.7 809.0 2431.7 1650.1 930.6 2580.6 3.7461 1.4994 5.245517000 352.37 0.001770 0.008364 1660.2 744.8 2405.0 1690.3 856.9 2547.2 3.8079 1.3698 5.177718000 357.06 0.001840 0.007489 1698.9 675.4 2374.3 1732.0 777.1 2509.1 3.8715 1.2329 5.104419000 361.54 0.001924 0.006657 1739.9 598.1 2338.1 1776.5 688.0 2464.5 3.9388 1.0839 5.022820000 365.81 0.002036 0.005834 1785.6 507.5 2293.0 1826.3 583.4 2409.7 4.0139 .9130 4.926921000 369.89 0.002207 0.004952 1842.1 388.5 2230.6 1888.4 446.2 2334.6 4.1075 .6938 4.801322000 373.80 0.002742 0.003568 1961.9 125.2 2087.1 2022.2 143.4 2165.6 4.3110 .2216 5.532722090 374.14 0.003155 0.003155 2029.6 0 2029.6 2099.3 0 2099.3 4.4298 0 4.4298

FIG. 24-29 (Contd)Saturated Steam: Pressure Table

24-36

FIG. 24-30Superheated Vapor

T

P = 10 kPa (45.81C) P = 50 kPa (81.33C) P = 100 kPa (99.63C)

v u h s v u h s v u h sSat. 14.674 2437.9 2584.7 8.1502 3.240 2483.9 2645.9 7.5939 1.6940 2506.1 2675.5 7.359450 14.869 2443.9 2592.6 8.1749100 17.196 2515.5 2687.5 8.4479 3.418 2511.6 2682.5 7.6958 1.6958 2506.7 2676.2 7.3614150 19.512 2587.9 2783.0 8.6882 3.889 2585.6 2780.1 7.9401 1.9364 2582.8 2776.4 7.6134200 21.825 2661.3 2879.5 8.9038 4.356 2659.9 2877.7 8.1580 2.172 2658.1 2875.3 7.8343250 24.136 2736.0 2977.3 9.1002 4.820 2735.0 2976.0 8.3556 2.406 2733.7 2974.3 8.0333300 26.445 2812.1 3076.5 9.2813 5.284 2811.3 3075.5 8.5373 2.639 2810.4 3074.3 8.2158400 31.063 2968.9 3279.6 9.6077 6.209 2968.5 3278.9 8.8642 3.103 2967.9 3278.2 8.5435500 35.679 3132.3 3489.1 9.8978 7.134 3132.0 3488.7 9.1546 3.565 3131.6 3488.1 8.8342600 40.295 3302.5 3705.4 10.1608 8.057 3302.2 3705.1 9.4178 4.028 3301.9 3704.7 9.0976700 44.911 3479.6 3928.7 10.4028 8.981 3479.4 3928.5 9.6599 4.490 3479.2 3928.2 9.3398800 49.526 3663.8 4159.0 10.6281 9.904 3663.6 4158.9 9.8852 4.952 3663.5 4158.6 9.5652900 54.141 3855.0 4396.4 10.8396 10.828 3854.9 4396.3 10.0967 5.414 3854.8 4396.1 9.77671000 58.757 4053.0 4640.6 11.0393 11.751 4052.9 4640.5 10.2964 5.875 4052.8 4640.3 9.97641100 63.372 4257.5 4891.2 11.2287 12.674 4257.4 4891.1 10.4859 6.337 4257.3 4891.0 10.16591200 67.987 4467.9 5147.8 11.4091 13.597 4467.8 5147.7 10.6662 6.799 4467.7 5147.6 10.34631300 72.602 4683.7 5409.7 11.5811 14.521 4683.6 5409.6 10.8382 7.260 4683.5 5409.5 10.5183


Sat. .8857 2529.5 2706.7 7.1272 .6058 2543.6 2725.3 6.9919 .4625 2553.6 2738.6 6.8959150 .9596 2576.9 2768.8 7.2795 .6339 2570.8 2761.0 7.0778 .4708 2564.5 2752.8 6.9299200 1.0803 2654.4 2870.5 7.5066 .7163 2650.7 2865.6 7.3115 .5342 2646.8 2860.5 7.1706250 1.1988 2731.2 2971.0 7.7086 .7964 2728.7 2967.6 7.5166 .5951 2726.1 2964.2 7.3789300 1.3162 2808.6 3071.8 7.8926 .8753 2806.7 3069.3 7.7022 .6548 2804.8 3066.8 7.5662400 1.5493 2966.7 3276.6 8.2218 1.0315 2965.6 3275.0 8.0330 .7726 2964.4 3273.4 7.8985500 1.7814 3130.8 3487.1 8.5133 1.1867 3130.0 3486.0 8.3251 .8893 3129.2 3484.9 8.1913600 2.013 3301.4 3704.0 8.7770 1.3414 3300.8 3703.2 8.5892 1.0055 3300.2 3702.4 8.4558700 2.244 3478.8 3927.6 9.0194 1.4957 3478.4 3927.1 8.8319 1.1215 3477.9 3926.5 8.6987800 2.475 3663.1 4158.2 9.2449 1.6499 3662.9 4157.8 9.0576 1.2372 3662.4 4157.3 8.9244900 2.706 3854.5 4395.8 9.4566 1.8041 3854.2 4395.4 9.2692 1.3529 3853.9 4395.1 9.13621000 2.937 4052.5 4640.0 9.6563 1.9581 4052.3 4639.7 9.4690 1.4685 4052.0 4639.4 9.33601100 3.168 4257.0 4890.7 9.8458 2.1121 4256.8 4890.4 9.6585 1.5840 4256.5 4890.2 9.52561200 3.399 4467.5 5147.3 10.0262 2.2661 4467.2 5147.1 9.8389 1.6996 4467.0 5146.8 9.70601300 3.630 4683.2 5409.3 10.1982 2.4201 4683.0 5409.0 10.0110 1.8151 4682.8 5408.8 9.8780


Sat .3749 2561.2 2748.7 6.8213 .3157 2567.4 2756.8 6.7600 .2404 2576.8 2769.1 6.6628200 .4249 2642.9 2855.4 7.0592 .3520 2638.9 2850.1 6.9665 .2608 2630.6 2839.3 6.8158250 .4744 2723.5 2960.7 7.2709 .3938 2720.9 2957.2 7.1816 .2931 2715.5 2950.0 7.0384300 .5226 2802.9 3064.2 7.4599 .4344 2801.0 3061.6 7.3724 .3241 2797.2 3056.5 7.2328350 .5701 2882.6 3167.7 7.6329 .4742 2881.2 3165.7 7.5464 .3544 2878.2 3161.7 7.4089400 .6173 2963.2 3271.9 7.7938 .5137 2962.1 3270.3 7.7079 .3843 2959.7 3267.1 7.5716500 .7109 3128.4 3483.9 8.0873 .5920 3127.6 3482.8 8.0021 .4433 3126.0 3480.6 7.8673600 .8041 3299.6 3701.7 7.3522 .6697 3299.1 3700.9 8.2674 .5018 3297.9 3699.4 8.1333700 .8969 3477.5 3925.9 8.5952 .7472 3477.0 3925.3 8.5107 .5601 3476.2 3924.2 8.3770800 .9896 3662.1 4156.9 8.8211 .8245 3661.8 4156.5 8.7367 .6181 3661.1 4155.6 8.6033900 1.0822 3853.6 4394.7 9.0329 .9017 3853.4 4394.4 8.9486 .6761 3852.8 4393.7 8.81531000 1.1747 4051.8 4639.1 9.2328 .9788 4051.5 4638.8 9.1485 .7340 4051.0 4638.2 9.01531100 1.2672 4256.3 4889.9 9.4224 1.0559 4256.1 4889.6 9.3381 .7919 4255.6 4889.1 9.20501200 1.3596 4466.8 5146.6 9.6029 1.1330 4466.5 5146.3 9.5185 .8497 4466.1 5145.9 9.38551300 1.4521 4682.5 5408.6 9.7749 1.2101 4682.3 5408.3 9.6906 .9076 4681.8 5407.9 9.5575


Sat .19444 2583.6 2778.1 6.5865 .16333 2588.8 2784.8 6.5233 .14084 2592.8 2790.0 6.4693200 .2060 2621.9 2827.9 6.6940 .16930 2612.8 2815.9 6.5898 .14302 2603.1 2803.3 6.4975250 .2327 2709.9 2942.6 6.9247 .19234 2704.2 2935.0 6.8294 .16350 2698.3 2927.2 6.7467300 .2579 2793.2 3051.2 7.1229 .2138 2789.2 3045.8 7.0317 .18228 2785.2 3040.4 6.9534350 .2825 2875.2 3157.7 7.3011 .2345 2872.2 3153.6 7.2121 .2003 2869.2 3149.5 7.1360400 .3066 2957.3 3263.9 7.4651 .2548 2954.9 3260.7 7.3774 .2178 2952.5 3257.5 7.3026500 .3541 3124.4 3478.5 7.7622 .2946 3122.8 3476.3 7.6959 .2521 3121.1 3474.1 7.6027600 .4011 3296.8 3697.9 8.0290 .3339 3295.6 3696.3 7.9435 .2860 3294.4 3694.8 7.8710700 .4478 3475.3 3923.1 8.2731 .3729 3474.4 3922.0 8.1881 .3195 3473.6 3920.8 8.1160800 .4943 3660.4 4154.7 8.4996 .4118 3659.7 4153.8 8.4148 .3528 3659.0 4153.0 8.3431900 .5407 3852.2 4392.9 8.7118 .4505 3851.6 4392.2 8.6272 .3861 3851.1 4391.5 8.55561000 .5871 4050.5 4637.6 8.9119 .4892 4050.0 4637.0 8.8274 .4192 4049.5 4636.4 8.75591100 .6335 4255.1 4888.6 9.1017 .5278 4254.6 4888.0 9.0172 .4524 4254.1 4887.5 8.94571200 .6798 4465.6 5145.4 9.2822 .5665 4465.1 5144.9 9.1977 .4855 4464.7 5144.4 9.12621300 .7261 4681.3 5407.4 9.4543 .6051 4680.9 5407.0 9.3698 .5186 4680.4 5606.5 9.2984

SymbolsUsedinSteamTables:Ppressure,kPa(abs);Tthermodynamictemperature,C;vspecificvolume,m3/kg;uspecificinternalenergy,kJ/kg;hspecificenthalpy,kJ/kgsspecificentropy,kJ/(kgK)AdaptedfromJosephH.Keenan,FrederickG.Keyes,PhilipG.Hill,andJoanG.Moore,SteamTables,(NewYork:JohnWiley&sons,Inc.,1969).

24-37

P = 1600 kPa (201.41C) P = 1800 kPa (207.15C) P = 2000 kPa (212.42C)Sat. .12380 2596.0 2794.0 6.4218 .11042 2598.4 2797.1 6.3794 .09963 2600.3 2799.5 6.3409225 .13287 2644.7 2857.3 6.5518 .11673 2636.6 2846.7 6.4808 .10377 2628.3 2835.8 6.4147250 .14184 2692.3 2919.2 6.6732 .12497 2686.0 2911.0 6.6066 .11144 2679.6 2902.5 6.5453300 .15862 2781.1 3034.8 6.8844 .14021 2776.9 3029.2 6.8226 .12547 2772.6 3023.5 6.7664350 .17456 2866.1 3145.4 7.0694 .15457 2863.0 3141.2 7.0100 .13857 2859.8 3137.0 6.9563400 .19005 2950.1 3254.2 7.2374 .16847 2947.7 3250.9 7.1794 .15120 2945.2 3247.6 7.1271500 .2203 3119.5 3472.0 7.5390 .19550 3117.9 3469.8 7.4825 .17568 3116.2 3467.6 7.4317600 .2500 3293.3 3693.2 7.8080 .2220 3292.1 3691.7 7.7523 .19960 3290.9 3690.1 7.7024700 .2794 3472.7 3919.7 8.0535 .2482 3471.8 3918.5 7.9983 .2232 3470.9 3917.4 7.9487800 .3086 3658.3 4152.1 8.2808 .2742 3657.6 4151.2 8.2258 .2467 3657.0 4150.3 8.1765900 .3377 3850.5 4390.8 8.4935 .3001 3849.9 4390.1 8.4386 .2700 3849.3 4389.4 8.38951000 .3668 4049.0 4635.8 8.6938 .3260 4048.5 4635.2 8.6391 .2933 4048.0 4634.6 8.59011100 .3958 4253.7 4887.0 8.8837 .3518 4253.2 4886.4 8.8290 .3166 4252.7 4885.9 8.78001200 .4248 4464.2 5143.9 9.0643 .3776 4463.7 5143.4 9.0096 .3398 4463.3 5142.9 8.96071300 .4538 4679.9 5406.0 9.2364 .4034 4679.5 5405.6 9.1818 .3631 4679.0 5405.1 9.1329


Sat. .07998 2603.1 2803.1 6.2575 .06668 2604.1 2804.2 6.1869 .05707 2603.7 2803.4 6.1253225 .08027 2605.6 2806.3 6.2639250 .08700 2662.6 2880.1 6.4085 .07058 2644.0 2855.8 6.2872 .05872 2623.7 2829.2 6.1749300 .09890 2761.6 3008.8 6.6438 .08114 2750.1 2993.5 6.5390 .06842 2738.0 2977.5 6.4461350 .10976 2851.9 3126.3 6.8403 .09053 2843.7 3115.3 6.7428 .07678 2835.3 3104.0 6.6579400 .12010 2939.1 3239.3 7.0148 .09936 2932.8 3230.9 6.9212 .08453 2926.4 3222.3 6.8405450 .13014 3025.5 3350.8 7.1746 .10787 3020.4 3344.0 7.0834 .09196 3015.3 3337.2 7.0052500 .13998 3112.1 3462.1 7.3234 .11619 3108.0 3456.5 7.2338 .09918 3103.0 3450.9 7.1572600 .15930 3288.0 3686.3 7.5960 .13243 3285.0 3682.3 7.5085 .11324 3282.1 3678.4 7.4339700 .17832 3468.7 3914.5 7.8435 .14838 3466.5 3911.7 7.7511 .12699 3464.3 3908.8 7.6837800 .19716 3655.3 4148.2 8.0720 .16414 3653.5 4145.9 7.9862 .14056 3651.8 4143.7 7.9134900 .21590 3847.9 4387.6 8.2853 .17980 3846.5 4385.9 8.1999 .154.02 3845.0 4384.1 8.12761000 .2346 4046.7 4633.1 8.4861 .19541 4045.4 4631.6 8.4009 .16743 4044.1 4630.1 8.32881100 .2532 4251.5 4884.6 8.6762 .21098 4250.3 4883.3 8.5912 .18080 4249.2 4881.9 8.51921200 .2718 4462.1 5141.7 8.8569 .22652 4460.9 5140.5 8.7720 .19415 4459.8 5139.3 8.70001300 .2905 4677.8 5404.0 9.0291 .24206 4676.6 5402.8 8.9442 .207.49 4675.5 5401.7 8.8723


Sat. .04978 2602.3 2801.4 6.0701 .04406 2600.1 2793.3 6.0198 .03944 2597.1 2794.3 5.9734275 .05457 2667.9 2886.2 6.2285 .04730 2650.3 2863.2 6.1401 .04141 2631.3 2838.3 6.0544300 .05884 2725.3 2960.7 6.3615 .05135 2712.0 2943.1 6.2828 .04532 2698.0 2924.5 6.2084350 .06645 2826.7 3092.5 6.5821 .05840 2817.8 3080.6 6.5131 .05194 2808.7 3068.4 6.4493400 .07341 2919.9 3213.6 6.7690 .06475 2913.3 3204.7 6.7047 .05781 2906.6 3195.7 6.6459450 .08002 3010.2 3330.3 6.9363 .07074 3005.0 3323.3 6.8746 .06330 2999.7 3316.2 6.8186500 .08643 3099.5 3445.3 7.0901 .07651 3095.3 3439.6 7.0301 .06857 3091.0 3433.8 6.9759600 .09885 3279.1 3674.4 7.3688 .08765 3276.0 3670.5 7.3110 .07869 3273.0 3665.5 7.2589700 .11095 3462.1 3905.9 7.6198 .09847 3459.9 3903.0 7.5631 .08849 3457.6 3900.1 7.5122800 .12287 3650.0 4141.5 7.8502 .10911 3648.3 4139.3 7.7942 .09811 3646.6 4137.1 7.7440900 .13469 3843.6 4382.3 8.0647 .11965 3842.2 4380.6 8.0091 .10762 3840.7 4378.8 7.95931000 .14645 4042.9 4628.7 8.2662 .13013 4041.6 4627.2 8.2108 .11707 4040.4 4625.7 8.16121100 .15817 4248.0 4880.6 8.4567 .14056 4246.8 4879.3 8.4015 .12648 4245.6 4878.0 8.35201200 .16987 4458.6 5138.1 8.6376 .15098 4457.5 5136.9 8.5825 .13587 4456.3 5135.7 8.53311300 .18156 4674.3 5400.5 8.8100 .16139 4673.1 5399.4 8.7549 .14526 4672.0 5398.2 8.7055


Sat. .03244 2589.7 2784.3 5.8892 .02737 2580.5 2772.1 5.8133 .02352 2569.8 2758.0 5.7432300 .03616 2667.2 2884.2 6.0674 .02947 2632.2 2838.4 5.9305 .02426 2590.9 2785.0 5.7906350 .04223 2789.6 3043.0 6.3335 .03524 2769.4 3016.0 6.2283 .02995 2747.7 2987.3 6.1301400 .04739 2892.9 3177.2 6.5408 .03993 2878.6 3158.1 6.4478 .03432 2863.8 3138.3 6.3634450 .05214 2988.9 3301.8 6.7193 .04416 2978.0 3287.1 6.6327 .03817 2966.7 3272.0 6.5551500 .05665 3082.2 3422.2 6.8803 .04814 3073.4 3410.3 6.7975 .04175 3064.3 3398.3 6.7240550 .06101 3174.6 3540.6 7.0288 .05195 3167.2 3530.9 6.9486 .04516 3159.8 3521.0 6.8778600 .06525 3266.9 3658.4 7.1677 .05565 3260.7 3650.3 7.0894 .04845 3254.4 3642.0 7.0206700 .07352 3453.1 3894.2 7.4234 .06283 3448.5 3888.3 7.3476 .05481 3443.9 3882.4 7.2812800 .08160 3643.1 4132.7 7.6566 .06981 3639.5 4128.2 7.5822 .06097 3636.0 4123.8 7.5173900 .08958 3837.8 4375.3 7.8727 .076.69 3835.0 4371.8 7.7991 .06702 3832.1 4368.3 7.73511000 .09749 4037.8 4622.7 8.0751 .08350 4035.3 4619.8 8.0020 .07301 4032.8 4616.9 7.93841100 .10536 4243.3 4875.4 8.2661 .09027 4240.9 4872.8 8.1933 .07896 4238.6 4870.3 8.13001200 .11321 4454.0 5133.3 8.4474 .09703 4451.7 5130.9 8.3747 .08489 4449.5 5128.5 8.31151300 .12106 4669.6 5396.0 8.6199 .10377 4667.3 5393.7 8.5473 .09080 4665.0 5391.5 8.4842


FIG. 24-30 (Contd)Superheated Vapor

24-38

P = 9000 kPa (303.40C) P = 10 000 kPa (311.06C) P = 12 500 kPa (327.89C)

Sat. .02048 2557.8 2742.1 5.6772 .018026 2544.4 2724.7 5.6141 .013495 2505.1 2673.8 5.4624325 .02327 2646.6 2856.0 5.8712 .019861 2610.4 5756.8350 .02580 2724.4 2956.6 6.0361 .02242 2699.2 2923.4 5.9443 .016126 2624.2 5711.8400 .02993 2848.4 3117.8 6.2854 .02641 2832.4 3096.5 6.2120 .02000 2789.3 3039.3 6.0417450 .03350 2955.2 3256.6 6.4844 .02975 2943.4 3240.9 6.4190 .02299 2912.5 3199.8 6.2719500 .03677 3055.2 3386.1 6.6576 .03279 3045.8 3373.7 6.5966 .02560 3021.7 3341.8 6.4618550 .03987 3152.2 3511.0 6.8142 .03564 3144.6 3500.9 6.7561 .02801 3125.0 3475.2 6.6290600 .04285 3248.1 3633.7 6.9589 .03837 3241.7 3625.3 6.9029 .03029 3225.4 3604.0 6.7810650 .04574 3343.6 3755.3 7.0943 .04101 3338.2 3748.2 7.0398 .03248 3324.4 3730.4 6.9218700 .04857 3439.3 3876.5 7.2221 .04358 3434.7 3870.5 7.1687 .03460 3422.9 3855.3 7.0536800 .05409 3632.5 4119.3 7.4596 .04859 3628.9 4114.8 7.4077 .03869 3620.0 4103.6 7.2965900 .05950 3829.2 4364.8 7.6783 .05349 3826.3 4361.2 7.6272 .04267 3819.1 4352.5 7.51821000 .06485 4030.3 4614.0 7.8821 .05832 4027.8 4611.0 7.8315 .04658 4021.6 4603.8 7.72371100 .07016 4236.3 4867.7 8.0740 .06312 4234.0 4865.1 8.0237 .05045 4228.2 4858.8 7.91651200 .07544 4447.2 5126.2 8.2556 .06789 4444.9 5123.8 8.2055 .05430 4439.3 5118.0 8.09871300 .08072 4662.7 5389.2 8.4284 .07265 4460.5 5387.0 8.3783 .05813 4654.8 5381.4 8.2717

P = 15 000 kPa (342.24C) P = 17 500 kPa (354.75C) P = 20 000 kPa (365.81C)

Sat. .010337 2455.5 2610.5 5.3098 .007920 2390.2 2528.8 5.1419 .005834 2293.0 2409.7 4.9269350 .011470 2520.4 2692.4 5.4421400 .015649 2740.7 2975.5 5.8811 .012447 2685.0 2902.9 5.7213 .009942 2619.3 2818.1 5.5540450 .018445 2879.5 3156.2 6.1404 .015174 2844.2 3109.7 6.0184 .012695 2806.2 3060.1 5.9017500 .02080 2996.6 3308.6 6.3443 .017358 2970.3 3274.1 6.2383 .014768 2942.9 3238.2 6.1401550 .02293 3104.7 3448.6 6.5199 .019288 3083.9 3421.4 6.4230 .016555 3062.4 3393.5 6.3348600 .02491 3208.6 3582.3 6.6776 .02106 3191.5 3560.1 6.5866 .018178 3174.0 3537.6 6.5048650 .02680 3310.3 3712.3 6.8224 .02274 3296.0 3693.9 6.7357 .019693 3281.4 3675.3 6.6582700 .02861 3410.9 3840.1 6.9572 .02434 3398.7 3824.6 6.8736 .02113 3386.4 3809.0 6.7993800 .03210 3610.9 4092.4 7.2040 .02738 3601.8 4081.1 7.1244 .02385 3592.7 4069.7 7.0544900 .03546 3811.9 4343.8 7.4279 .03031 3804.7 4335.1 7.3507 .02645 3797.5 4326.4 7.28301000 .03875 4015.4 4596.6 7.6348 .03316 4009.3 4589.5 7.5589 .02897 4003.1 4582.5 7.49251100 .04200 4222.6 4852.6 7.8283 .03597 4216.9 4846.4 7.7531 .03145 4211.3 4840.2 7.68741200 .04523 4433.8 5112.3 8.0108 .03876 4428.3 5106.6 7.9360 .03391 4422.8 5101.0 7.87071300 .04845 4649.1 5376.0 8.1840 .04154 4643.5 5370.5 8.1093 .03636 4638.0 5365.1 8.0442

P = 25 000 kPa P = 30 000 kPa P = 35 000 kPa

375 .0019731 1798.1 1848.0 4.0320 .001789 1737.8 1791.5 3.9305 .0017003 1702.9 1762.4 3.8722400 .006004 2430.1 2580.2 5.1418 .002790 2067.4 2151.1 4.4728 .002100 1914.1 1987.6 4.2126425 .007881 2609.2 2806.3 5.4723 .005303 2455.1 2614.2 5.1504 .003428 2253.4 2373.4 4.7747450 .009162 2720.7 2949.7 5.6744 .006735 2619.3 2821.4 5.4424 .004961 2498.7 2672.4 5.1962500 .011123 2884.3 3162.4 5.9592 .008678 2820.7 3081.1 5.7905 .006927 2751.9 2994.4 5.6282550 .012724 3017.5 3335.6 6.1765 .010168 2970.3 3275.4 6.0342 .008345 2921.0 3213.0 5.9026600 .014137 3137.9 3491.4 6.3602 .011446 3100.5 3443.9 6.2331 .009527 3062.0 3395.5 6.1179650 .015433 3251.6 3637.4 6.5229 .012596 3221.0 3598.9 6.4058 .010575 3189.8 3559.9 6.3010700 .016646 3361.3 3777.5 6.6707 .013661 3335.8 3745.6 6.5605 .011533 3309.8 3713.5 6.4631800 .018912 3574.3 4047.1 6.9345 .015623 3555.5 4024.2 6.8332 .013278 3536.7 4001.5 6.7450900 .021045 3783.0 4309.1 7.1680 .017448 3768.5 4291.9 7.0718 .014883 3754.0 4274.9 6.98861000 .02310 3990.9 4568.5 7.3802 .019196 3978.8 4554.7 7.2867 .016410 3966.7 4541.1 7.20641100 .02512 4200.4 4828.2 7.5765 .020903 4189.2 4816.3 7.4845 .017895 4178.3 4804.6 7.40571200 .02711 4412.0 5089.9 7.7605 .022589 4401.3 5079.0 7.6692 .019360 4390.7 5068.3 7.59101300 .02910 4626.9 5354.4 7.9342 .024266 4616.0 5344.0 7.8432 .020815 4605.1 5333.6 7.7653

P = 40 000 kPa P = 50 000 kPa P = 60 000kPa

375 .0016407 1677.1 1742.8 3.8290 .0015594 1638.6 1716.6 3.7639 .0015028 1609.4 1699.5 3.7141400 .0019077 1854.6 1930.9 4.1135 .0017309 1788.1 1874.6 4.0031 .0016335 1745.4 1843.4 3.9318425 .002532 2096.9 2198.1 4.5029 .002007 1959.7 2060.0 4.2734 .0018165 1892.7 2001.7 4.1626450 .003693 2365.1 2512.8 4.9459 .002486 2159.6 2284.0 4.5884 .002085 2053.9 2179.0 4.4121500 .005622 2678.4 2903.3 5.4700 .003892 2525.5 2720.1 5.1726 .002956 2390.6 2567.9 4.9321550 .006984 2869.7 3149.1 5.7785 .005118 2763.6 3019.5 5.5485 .003956 2658.8 2896.2 5.3441600 .008094 3022.6 3346.4 6.0114 .006112 2942.0 3247.6 5.8178 .004834 2861.1 3151.2 5.6452650 .009063 3158.0 3520.6 6.2054 .006966 3093.5 3441.8 6.0342 .005595 3028.8 3364.5 5.8829700 .009941 3283.6 3681.2 6.3750 .007727 3230.5 3616.8 6.2189 .006272 3177.2 3553.5 6.0824800 .011523 3517.8 3978.7 6.6662 .009076 3479.8 3933.6 6.5290 .007459 3441.5 3889.1 6.4109900 .012962 3739.4 4257.9 6.9150 .010283 3710.3 4224.4 6.7882 .008508 3681.0 4191.5 6.68051000 .014324 3954.6 4527.6 7.1356 .011411 3930.5 4501.1 7.0146 .009480 3906.4 4475.2 6.91271100 .015642 4167.4 4793.1 7.3364 .012496 4145.7 4770.5 7.2184 .010409 4124.1 4748.6 7.11951200 .016940 4380.1 5057.7 7.5224 .013561 4359.1 5037.2 7.4058 .011317 4338.2 5017.2 7.30831300 .018229 4594.3 5323.5 7.6969 .014616 4572.8 5303.6 7.5808 .012215 4551.4 5284.3 7.4837


FIG. 24-30 (Contd)Superheated Vapor

Table of ContentsViewing RecommendationsSearch the Data BookHelpSection 24 Thermodynamic Properties DEFINITIONS OF WORDS AND PHRASES USED IN INSTRUMENTATIONENTHALPY BEHAVIORIdeal Gas State Enthalpies

CHANGE OF ENTHALPY WITHPRESSUREEXAMPLE CALCULATION USING ENTHALPY CORRELATIONENTROPY CORRELATIONEXAMPLE CALCULATION USING ENTROPY CORRELATIONENTHALPY AND ENTROPY DATAPure CO2Mixtures of CO2 with H2SOxygen, Nitrogen, and Helium

USES FOR P-H CHARTSREFERENCESBIBLIOGRAPHY

FIGURESFIG. 24-1: NomenclatureFIG. 24-2: Influence of Pressure on Enthalpy for Typical Natural Gas StreamsFIG. 24-3: Ideal-Gas-State Enthalpy of Pure ComponentsFIG. 24-4: Ideal-Gas-State Enthalpy of Pure ComponentsFIG. 24-5: Ideal-Gas-State Enthalpy of Petroleum FractionsFIG. 24-6: Effect of Pressure on Enthalpy (Simple Fluid)FIG. 24-7: Effect of Pressure on Enthalpy (Correction for Real Fluids)FIG. 24-8: Example Enthalpy Calculation FIG. 24-9: Example Entropy Calculation FIG. 24-10: Ideal Gas State Entropy of Pure Components FIG. 24-11: Effect of Pressure on Entropy (Simple Fluid) FIG. 24-12: Effect of Pressure on Entropy (Correction for Real Fluids) FIG. 24-13: Sample Isenthalpic Blowdown Paths FIG. 24-14: Sample Multi-Stage Compression Path with Interstage Cooling and Recycle FIG. 24-15: Carbon Dioxide P-H DiagramFIG. 24-16: Nitrogen P-H Diagram FIG. 24-17: Methane P-H Diagram FIG. 24-18: Ethane P-H Diagram FIG. 24-19: Ethylene P-H Diagram FIG. 24-20: Propane P-H Diagram FIG. 24-21: Propylene P-H Diagram FIG. 24-22: i-Butane P-H Diagram FIG. 24-23: n-Butane P-H Diagram FIG. 24-24: i-Pentane P-H Diagram FIG. 24-25: n-Pentane P-H Diagram FIG. 24-26: Oxygen P-H Diagram FIG. 24-27: Thermodynamic Properties of Water FIG. 24-28: Thermodynamic Properties of Water FIG. 24-29: Saturated Steam: Temperature Table FIG. 24-30: Superheated Vapor

M24 - Thermodynamic Properties

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